CN105819404A - Zero-discharge startup and shutdown technology of sulfur recovering device - Google Patents

Zero-discharge startup and shutdown technology of sulfur recovering device Download PDF

Info

Publication number
CN105819404A
CN105819404A CN201610146533.XA CN201610146533A CN105819404A CN 105819404 A CN105819404 A CN 105819404A CN 201610146533 A CN201610146533 A CN 201610146533A CN 105819404 A CN105819404 A CN 105819404A
Authority
CN
China
Prior art keywords
tail gas
sulfur
hydrogenation reactor
during
introducing
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
CN201610146533.XA
Other languages
Chinese (zh)
Inventor
杨想全
高炬
李铁军
周葆红
李维义
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Shandong Sunway Petrochemical Engineering Co Ltd
Original Assignee
Shandong Sunway Petrochemical Engineering Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Shandong Sunway Petrochemical Engineering Co Ltd filed Critical Shandong Sunway Petrochemical Engineering Co Ltd
Priority to CN201610146533.XA priority Critical patent/CN105819404A/en
Publication of CN105819404A publication Critical patent/CN105819404A/en
Pending legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/02—Preparation of sulfur; Purification
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/30—Alkali metal compounds
    • B01D2251/304—Alkali metal compounds of sodium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/40—Alkaline earth metal or magnesium compounds
    • B01D2251/402—Alkaline earth metal or magnesium compounds of magnesium
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Abstract

The invention belongs to the technical fields of sulfur recovery and tail gas processing, and specifically relates to a zero-discharge startup and shutdown technology of sulfur recovering device. The technology comprises the following steps: (1) during the furnace drying period, directly introducing the generated flue gas into an alkali absorbing tower; (2) during the converter temperature rising period, burning the tail gas from a tail gas liquid separation tank in an incinerator, introducing the high temperature flue gas into a tail gas waste heat boiler to recover the waste heat, and finally introducing the flue gas into an alkali absorbing tower; (3) during the pre-sulfurization period of a catalyst in a hydrogenation reactor, controlling the concentration of a catalyst, which is used in a hydrogenation reactor for pre-sulfurization of hydrogen sulfide in sulfur production process gas, by a ratio analyzing instrument, introducing hydrogenation tail gas into an incinerator after the tail gas goes through a quench tower, burning the tail gas, and then introducing the tail gas into an alkali absorbing tower to absorb SO2; (4) during the shutdown sulfur blowing and hydrogenation reactor catalyst passivation period, introducing the shutdown tail gas into an incinerator after the tail gas goes through a quench tower, burning the tail gas, and then introducing the tail gas into an alkali absorbing tower to absorb SO2. The technology can control the density of discharge SO2 to be less than 100 mg/Nm3.

Description

Sulfur recovery unit zero-emission shutting down technique
Technical field
The invention belongs to sulphur recovery and tail gas disposal technique field, be specifically related to a kind of sulfur recovery unit zero-emission shutting down technique, particularly to the technique controlling atmosphere pollution zero-emission in a kind of sulfur recovery unit shutting down and hydrogenation reactor pre-vulcanization process.
Background technology
Along with global environmental protection regulation, regulations tend to strict, sulfur recovery unit has become Petrochemical Enterprises and coal chemical industry enterprises produces indispensable environmental protecting device.New " petrochemical industry pollutant emission standard " GB31570-2015 regulation promulgated, from 1 day July in 2017, sulfur recovery unit pollutant emission was performed by new standard, newly-built sulfur recovery unit SO2Concentration of emission should be less than 400mg/Nm3, atmospheric environment capacity is less, ecological environment frailty, is susceptible to great environmental pollution problem and needs to take the area of special protection measure, sulfur recovery unit SO2Concentration of emission should be less than 100mg/Nm3.Local government considers SO2Prediction emission and environmental protection pressure, atmosphere pollution SO of sulfur recovery unit2Concentration of emission is substantially by less than 100mg/Nm3Perform, conventional Crouse+Scott+amine absorption regeneration+burning can not meet requirement, it is primarily due to the complex reaction that amine absorption is MDEA and hydrogen sulfide, limited by molecular balance, it is impossible to reach the requirement of discharge, by increasing the circulating load of amine liquid and improving the lean degree of amine liquid, the investment and the energy consumption that increase are the biggest, it cannot be guaranteed that during device fluctuation can qualified discharge, and alkali liquor absorption is acid-base reaction, response speed is fast and ratio more thoroughly.Sulfur recovery unit needs to increase alkali liquor absorption, and total process route is: Crouse+Scott+amine absorption regeneration+burning+alkali liquor absorption.SO during sulfur recovery unit is discharged into air during shutting down2Concentration be 2000mg/Nm3～20000mg/Nm3, not only pollute environment, and cause the strong dissatisfaction of the masses around.
Summary of the invention
The problem that new standard " petrochemical industry pollutant emission standard " GB31570-2015 specifies can not be reached for solving the existing technique of sulfur recovery unit, the present invention provides the technique controlling atmosphere pollution zero-emission in a kind of sulfur recovery unit zero-emission shutting down technique, i.e. sulfur recovery facility shutting down and hydrogenation reactor pre-vulcanization process.Described technique can meet the requirement of atmosphere pollution zero-emission, simplifies operating process simultaneously, saves investment, solves shutting down period SO2The realistic problem of discharge severe overweight, by SO2Emission control at 100mg/Nm3Below.
The present invention adopts the following technical scheme that
A kind of sulfur recovery unit zero-emission shutting down technique, heats up including the baker that goes into operation, converter, sulfur and hydrogenation reactor catalyst structure are blown in hydrogenation reactor presulfiding of catalyst and shut-down, wherein,
1. going into operation during baker, baker flue gas directly enters alkali liquor absorption tower；
2., during converter heats up, after tail gas separatory tank carrys out tail gas entrance incinerator burning, gained high-temperature flue gas is through tail gas waste heat boiler recovery waste heat laggard alkali liquor absorption tower；
3., during hydrogenation reactor presulfiding of catalyst, with the hydrogen sulfide presulfurization hydrogenation reactor catalyst in sulfur Process Gas processed, by its concentration of ratio Analysis instrument control system, hydrogenation tail gas is introduced before chilling tower after incinerator burns and is absorbed SO through alkali liquor absorption tower2；
4. stopping work during blowing sulfur and hydrogenation reactor catalyst structure, shut-down tail gas is introduced before chilling tower after incinerator burns and is absorbed SO through alkali liquor absorption tower2。
In absorption tower, alkali liquor uses NaOH or Mg (OH)2。
The fire box temperature of incinerator is 550～650 DEG C, purifies H remaining in gas2S is combusted as SO2, remain H2CO is become with hydrocarbon fuel2And H2O。
H in sulfur Process Gas processed is controlled during hydrogenation reactor presulfurization2The volumetric concentration of S is less than 5%.
Compared with prior art, the invention have the advantages that
(1) going into operation during baker, baker flue gas directly enters caustic wash tower, before discharge by issuable SO2Absorb cleanly.Prior art is directly to arrange air or chimney, and sulfur recovery unit, in addition to not having sulfur simple substance and sulfide in go into operation for the first time sulfur stove processed and waste heat boiler, goes into operation later and all can have sulfur simple substance and sulfide, directly row's atmospheric pollution environment；
(2) existing hydrogenation reactor presulfurization flow process is by circulating fan pressurization cycle presulfurization, the outlet of circulating air self-absorption tower is after circulating air surge tank buffering separatory, through circulating fan supercharging Posterior circle presulfurization, unnecessary circulating air enters tail gas furnace after voltage-controlled valve and burns, i.e. it is provided with special presulfurization flow process and equipment, and presulfurization only goes into operation with 24 hours, remaining time does not leaves unused in all senses.The present invention is not separately provided presulfurization flow process, and device went into operation to the presulfurization stage, opens up into the flow process of hydrogenation reactor, and former ad hoc presulfurization equipment, pipeline, instrument and regulation valve can be cancelled.
(3) presulfurization flow process the earliest is owing to Process Gas needs are through over-quenching tower → circulating air surge tank → circulating fan → heater exhaust gas → hydrogenation reactor, elemental sulfur therein, H2S and SO2Chilling tower blocking in start-up process can be caused.Therefore, from cleaning sour gas line, individually drawing sour gas later and enter hydrogenation reactor presulfurization, although so avoiding the blocking of chilling tower, but being the introduction of high poison harm medium H2S, improves the risk class of subsequent technique.The present invention uses sulfur Process Gas processed to carry out presulfurization, there are not the problems referred to above.
(4) sulfur recovery unit is stopped work needs to blow sulfur, with air by elemental sulfur remain in system and sulfide stripping out, absorbs SO owing to not stopping work2Facility, cause the SO that downtime sulfur recovery unit discharges2The SO of discharge during severe overweight, and catalyst structure2Also severe overweight, the present invention utilizes alkali liquor absorption tower to meet qualified discharge requirement.
Accompanying drawing explanation
Fig. 1 is sulfur recovery unit zero-emission shutting down process flow diagram of the present invention.
Detailed description of the invention
Below in conjunction with accompanying drawing, the present invention will be further described:
The present invention adopts the following technical scheme that
As it is shown in figure 1, a kind of sulfur recovery unit zero-emission shutting down technique, heat up including the baker that goes into operation, converter, sulfur and hydrogenation reactor catalyst structure are blown in hydrogenation reactor presulfiding of catalyst and shut-down, wherein,
1. going into operation during baker, baker flue gas directly enters alkali liquor absorption tower；
2., during converter heats up, after tail gas separatory tank carrys out tail gas entrance tail gas furnace burning, gained high-temperature flue gas is through tail gas waste heat boiler recovery waste heat laggard alkali liquor absorption tower；
3., during hydrogenation reactor presulfiding of catalyst, with the hydrogen sulfide presulfurization hydrogenation reactor catalyst in sulfur Process Gas processed, by its concentration of ratio Analysis instrument control system, hydrogenation tail gas is introduced before chilling tower after incinerator burns and is absorbed SO through alkali liquor absorption tower2；
4. stopping work during blowing sulfur and hydrogenation reactor catalyst structure, shut-down tail gas is introduced before chilling tower after incinerator burns and is absorbed SO through alkali liquor absorption tower2。
Wherein, in absorption tower, alkali liquor uses NaOH, and the fire box temperature of incinerator is 550～650 DEG C, H in sulfur Process Gas processed during hydrogenation catalyst presulfurizing2The volumetric concentration of S is less than 5%.
Described technique solves shutting down period SO2The realistic problem of discharge severe overweight, by SO2Emission control at 100mg/Nm3Below.

Claims (4)

1. a sulfur recovery unit zero-emission shutting down technique, it is characterised in that the baker that includes going into operation, converter heat up, sulfur and hydrogenation reactor catalyst structure are blown in hydrogenation reactor presulfiding of catalyst and shut-down, wherein,
1. going into operation during baker, baker flue gas directly enters alkali liquor absorption tower；
2., during converter heats up, after tail gas separatory tank carrys out tail gas entrance incinerator burning, gained high-temperature flue gas is through tail gas waste heat boiler recovery waste heat laggard alkali liquor absorption tower；
3., during hydrogenation reactor presulfiding of catalyst, with the hydrogen sulfide presulfurization hydrogenation reactor catalyst in sulfur Process Gas processed, by its concentration of ratio Analysis instrument control system, hydrogenation tail gas is introduced before chilling tower after incinerator burns and is absorbed SO through alkali liquor absorption tower2；
4. stopping work during blowing sulfur and hydrogenation reactor catalyst structure, shut-down tail gas is introduced before chilling tower after incinerator burns and is absorbed SO through alkali liquor absorption tower2。
A kind of sulfur recovery unit zero-emission shutting down technique the most according to claim 1, it is characterised in that in alkali liquor absorption tower, alkali liquor uses NaOH or Mg (OH)2。
A kind of sulfur recovery unit zero-emission shutting down technique the most according to claim 1, it is characterised in that the fire box temperature of incinerator is 570～650 DEG C.
A kind of sulfur recovery unit zero-emission shutting down technique the most according to claim 1, it is characterised in that control H in sulfur Process Gas processed during hydrogenation reactor presulfurization2The volumetric concentration of S is less than 5%.
CN201610146533.XA 2016-03-15 2016-03-15 Zero-discharge startup and shutdown technology of sulfur recovering device Pending CN105819404A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201610146533.XA CN105819404A (en) 2016-03-15 2016-03-15 Zero-discharge startup and shutdown technology of sulfur recovering device

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201610146533.XA CN105819404A (en) 2016-03-15 2016-03-15 Zero-discharge startup and shutdown technology of sulfur recovering device

Publications (1)

Publication Number Publication Date
CN105819404A true CN105819404A (en) 2016-08-03

Family

ID=56987844

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201610146533.XA Pending CN105819404A (en) 2016-03-15 2016-03-15 Zero-discharge startup and shutdown technology of sulfur recovering device

Country Status (1)

Country Link
CN (1) CN105819404A (en)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110756195A (en) * 2018-07-27 2020-02-07 中国石油化工股份有限公司 Vulcanization type hydrogenation catalyst, preparation method thereof and green start-up method of sulfur device
CN112299378A (en) * 2019-08-02 2021-02-02 中国石油化工股份有限公司 Sulfur recovery device filled with sulfurized hydrogenation catalyst and start-up method
CN112299379A (en) * 2019-08-02 2021-02-02 中国石油化工股份有限公司 Sulfur recovery device filled with oxidation state hydrogenation catalyst and start-up method
CN113860266A (en) * 2020-06-30 2021-12-31 中国石油化工股份有限公司 Startup method of sulfur recovery process
CN114076321A (en) * 2021-11-15 2022-02-22 镇海石化工程股份有限公司 Method for treating petrochemical VOCs waste gas by using sulfur recovery device incinerator
CN115594154A (en) * 2021-07-09 2023-01-13 中国石油化工股份有限公司（Cn） Sulfur recovery device capable of realizing green shutdown and shutdown sulfur blowing method thereof

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA2037842A1 (en) * 1990-03-13 1991-09-14 James D. Seamans Method of presulfiding a hydrotreating, hydrocracking or tail gas treating catalyst
CN202829575U (en) * 2012-08-06 2013-03-27 中国石油化工股份有限公司 Sulfur recycling device
CN103159187A (en) * 2013-03-27 2013-06-19 山东三维石化工程股份有限公司青岛分公司 Shutdown technique of cleaner production of sulfur recovery and tail gas treatment device
CN103566730A (en) * 2012-08-06 2014-02-12 中国石油化工股份有限公司 Method for treating sulfur removal sweeping tail gas produced in shutdown process of sulfur recovery device

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA2037842A1 (en) * 1990-03-13 1991-09-14 James D. Seamans Method of presulfiding a hydrotreating, hydrocracking or tail gas treating catalyst
CN202829575U (en) * 2012-08-06 2013-03-27 中国石油化工股份有限公司 Sulfur recycling device
CN103566730A (en) * 2012-08-06 2014-02-12 中国石油化工股份有限公司 Method for treating sulfur removal sweeping tail gas produced in shutdown process of sulfur recovery device
CN103159187A (en) * 2013-03-27 2013-06-19 山东三维石化工程股份有限公司青岛分公司 Shutdown technique of cleaner production of sulfur recovery and tail gas treatment device

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
LYFLLH123: "硫磺回收尾气处理装置开工停工指南", 《百度文库》 *
M. RAMESHNI: "克劳斯尾气碱洗涤与生产硫酸的比较", 《硫酸工业》 *

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110756195A (en) * 2018-07-27 2020-02-07 中国石油化工股份有限公司 Vulcanization type hydrogenation catalyst, preparation method thereof and green start-up method of sulfur device
CN112299378A (en) * 2019-08-02 2021-02-02 中国石油化工股份有限公司 Sulfur recovery device filled with sulfurized hydrogenation catalyst and start-up method
CN112299379A (en) * 2019-08-02 2021-02-02 中国石油化工股份有限公司 Sulfur recovery device filled with oxidation state hydrogenation catalyst and start-up method
CN112299378B (en) * 2019-08-02 2022-03-22 中国石油化工股份有限公司 Sulfur recovery device filled with sulfurized hydrogenation catalyst and start-up method
CN113860266A (en) * 2020-06-30 2021-12-31 中国石油化工股份有限公司 Startup method of sulfur recovery process
CN113860266B (en) * 2020-06-30 2023-06-16 中国石油化工股份有限公司 Method for starting sulfur recovery process
CN115594154A (en) * 2021-07-09 2023-01-13 中国石油化工股份有限公司（Cn） Sulfur recovery device capable of realizing green shutdown and shutdown sulfur blowing method thereof
CN115594154B (en) * 2021-07-09 2023-12-05 中国石油化工股份有限公司 Sulfur recovery device capable of realizing green shutdown and shutdown sulfur blowing method thereof
CN114076321A (en) * 2021-11-15 2022-02-22 镇海石化工程股份有限公司 Method for treating petrochemical VOCs waste gas by using sulfur recovery device incinerator

Similar Documents

Publication Publication Date Title
CN105819404A (en) Zero-discharge startup and shutdown technology of sulfur recovering device
CN103055675B (en) Industrial smoke comprehensive treatment system and method based on advanced oxidation
CN202953829U (en) Acid gas desulfurizing device
CN105327599B (en) The processing method of molten sulfur degasification exhaust gas
CN111534335A (en) Blast furnace gas hydrolysis and dry-process fine desulfurization treatment system and method
CN103480252A (en) Hydrogen sulfide-containing acid gas treatment method
CN105214478A (en) The integral process of a kind of coke oven flue exhuast gas desulfurization denitration and waste heat recovery
US20170274324A1 (en) Claus unit treatment of shutdown tail gas
CN205505013U (en) Waste liquid, useless burning furnace flue gas processing system that burns admittedly
CN105797581A (en) System and process for utilizing coke oven flue gas desulfurization and denitrification waste heat
CN203816509U (en) Desulfuration and denitration system for low temperature coke oven exhaust
CN209652260U (en) A kind of Crouse's sulphur recovery and exhaust treatment system
CN105797562A (en) Two-section type double-ammonia-process integrated desulfurization and denitration system for coking flue gas
CN210973883U (en) Sulfur recovery device is blown in circulation
CN208852689U (en) A kind of Novel flue gas desulphurization system
CN107990335A (en) A kind of environment-friendly and energy-efficient industrial waste gas burning processing device
CN105318342B (en) A kind for the treatment of process of industrial smoke
EP3036480B1 (en) Arrangement and method for flue gas stream bypass during selective catalytic reduction
CN110793044A (en) Incineration device and method for treating sulfur recovery tail gas
CN207822774U (en) A kind of hydrogen sulfide containing VOCs exhaust treatment systems
CN110115929A (en) A kind of sulfur recovery facility sour gas alkali washing process
CN205730894U (en) A kind of low-temperature denitration wet method sulphur removing and dust removing also ensures the system that chimney is hot standby
CN209651900U (en) A kind of Crouse's sulfur recovery system
CN213824161U (en) Tail gas treatment equipment in hydrogenation catalyst burning treatment process
CN207137667U (en) A kind of reclamation of stack gas afterheat and the integrated apparatus of desulfurization

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
RJ01 Rejection of invention patent application after publication

Application publication date: 20160803

RJ01 Rejection of invention patent application after publication